US3037848A - Fluidized-bed reactor - Google Patents

Fluidized-bed reactor Download PDF

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Publication number
US3037848A
US3037848A US767557A US76755758A US3037848A US 3037848 A US3037848 A US 3037848A US 767557 A US767557 A US 767557A US 76755758 A US76755758 A US 76755758A US 3037848 A US3037848 A US 3037848A
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United States
Prior art keywords
bed
solids
chamber
tubular means
gas
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Expired - Lifetime
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US767557A
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English (en)
Inventor
Jr William L Davis
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United States Steel Corp
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United States Steel Corp
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Publication date
Priority to BE572997D priority Critical patent/BE572997A/xx
Application filed by United States Steel Corp filed Critical United States Steel Corp
Priority to US767557A priority patent/US3037848A/en
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/386—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only internally, i.e. the particles rotate within the vessel

Definitions

  • This invention relates to an improved solids discharge device for a fluidized bed reactor.
  • An object of my invention is to provide an improved solids discharge device which minimizes chances of incompletely reacted particles being discharged from a fluidized bed.
  • a further object is to provide a solids discharge device which takes solids from the most completely reacted region of a bed and affords further opportunity for them to react before actually removing them from the reactor.
  • a further object is to provide an improved solids discharge device which facilitates both adjustment in the depth of bed in a reactor and removal of the entire bed when necessary.
  • a further object is to provide an improved solids discharge device which enables the depth of bed to be adjusted downwardly from a predetermined normal level, as well as upwardly.
  • the single FIGURE is a diagrammatic vertical sectional view of a reactor equipped with a discharge device in accordance with my invention.
  • the FIGURE shows a fluidized bed reactor 10, which apart from my novel discharge device, can be of conventional construction.
  • a gas inlet 12 leads to the bottom of the reactor and a gas outlet 13 extends from the top.
  • the outlet is equipped with a conventional cyclone dust collector 14 and a shutoff valve 15, which is always open during operation of the reactor and is closed only when the contents of the reactor are to be emptied, as hereinafter explained.
  • a perforate horizontal partition 16 extends across the lower portion of the reactor above the gas inlet and supports a fluidized bed B of finely divided solid particles.
  • the reactor has a freeboard space F above the bed. Solids enter the bed through any conventional feeder indicated diagrammatically at 17.
  • the feeder commonly is a vertical pipe extending downwardly from the other reactor; otherwise the feeder 3fi3748 Patented June 5, 1962 may be a screw conveyor or a sloping pipe.
  • the feeder preferably introduces solids near one side Wall of the reactor, and when used in combination with my discharge device, near the top of the bed.
  • My novel discharge device comprises a vertical pipe 18 which is located at the side of the reactor opposite the feeder and extends from the bottom of the bed B just above partition 16 to a height within the freeboard F well above the maximum height of the bed.
  • Pipe 18 has a minimum diameter of about 2 inches enabling solids therein to remain fluidized, but has a relatively large height-to-diameter ratio to minimize vertical back-mixing of solids therein.
  • the pipe can be supported Within the reactor in any suitable way, such as by braces 19 depending from the top wall of the reactor and braces 20 upstanding from partition 16.
  • a downwardly sloping overflow pipe 21 extends from the intermediate portion of pipe 13 through the side wall of the reactor.
  • the effective height-to-diameter ratio of pipe 18 measured from its lower end to the overflow pipe 21 should be at least 10/ 1 and preferably in the range 15/1 to 20/1.
  • the overflow contains a shutoff valve 22.
  • a cone-type plug valve 23 is mounted for vertical movement above the upper end of pipe 18 and is adapted to restrict flow of gas from the pipe for adjusting the bed depth upwardly from its normal level or for emptying the reactor, as hereinafter explained.
  • an inlet pipe 24, which contains a normally closed Valve 25, leads to the lower portion of pipe 18 and is adapted to admit gas for adjusting the bed depth downwardly from its normal level.
  • valve 15 I and 22 are open in order not to interfere with escape of gas and solids from the reactor.
  • the gas fluidizes the solids in bed B and at the same time reacts in some way therewith.
  • the solids feeding into the reactor can be iron oxide, the gas a reductant therefor, and the solids discharging from the reactor a reduced product, such as metallic iron or a lower oxide.
  • the solids and/ or gas can be preheated if required for the reaction, or the reactor can be equipped with heating or cooling means if needed, all of which are known expedients in the art.
  • Solids near the bottom of the bed enter the lower end of pipe 18. As already explained, solids in this region tend to be the most completely reacted. Upcurrents of gas also enter this pipe and maintain solids therein fluidized and tend to react further therewith as the gas and solids flow upwardly together.
  • Sinc pipe 18 has a large effective depth-to-diameter ratio which limits vertical back-mixing, particles in the upper portion of the bed within the pipe now tend to be the most completely reacted. These particles overflow through the overflow pipe 21 for appropriate subsequent treatment.
  • valve 23 is positioned far enough above pipe 18 not to restrict escape of gas and valve 25 is closed, the top of bed B remains at a normal level N even with the line along which the overflow 21 intersects pipe 18.
  • valve 23 or 25 is adjusted to change the pressure drop of gas passing through pipe 18.
  • the pressure drop through bed B of course adjusts itself so that it again becomes equal to that through pipe 18; hence such adjustment changes the level of bed B to equalize the two pressure drops.
  • valve 23 is lowered to where it restricts escape of gas from pipe 18, thus increasing the pressure drop through this pipe.
  • the immediate effect is to lower the depth of solids in pipe 18 below the overflow 21; solids actually return from pipe 18 into bed B. As solids continue to enter bed B through the right chamber,
  • valves 15, 23 and 25 fully closed. Gas continues to enter the reactor through inlet 12 and causes pressure within the reactor to increase. The pressure increase can be relieved only by escape of gas through the overflow pipe 21. In thus escaping, the gas carries solids from the bed after the fashion of a dense phase pneumatic conveyor.
  • a reactor which includes walls forming an upa perforate horizontal partition extending across the lower portion of said chamber for supporting a fluidized bed of finely divided solids and permitting vertical back mixing thereof, which bed has predetermined normal, minimum and maximum operating levels, said chamber having a freedboard space above the bed when the bed is at any of its operating levels, means for feeding solids to the upper portion or" the bed, and means for passing upcurrents of a fluidizing gas through said partition and thence through the bed to react with the solids therein, said chamber having an outlet for the gas above the bed, the combination therewith of a discharge device comprising tubular means supported within said chamber and having a lower end above said partition near the bottom of the space occupied by the bed and an upper end in said freeboard space above the maximum operating level of the bed, both ends of said tubular means being open allowing solids from the bottom portion of the bed to enter directly and also allowing fluidizing gas to pass therethrough and continue its reaction with solids which have entered the tubular means, thus carrying the reaction more nearly toward completion, the
  • a combination as defined in claim 1 including an inlet for introducing a supplementary supply of gas to the lower portion of said tubular means, said valve and said inlet cooperating respectively to raise or to lower the pressure drop of gas passing through said tubular means, thereby raising or lowering the depth of bed in said reactor from said normal level.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
US767557A 1958-10-16 1958-10-16 Fluidized-bed reactor Expired - Lifetime US3037848A (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
BE572997D BE572997A (it) 1958-10-16
US767557A US3037848A (en) 1958-10-16 1958-10-16 Fluidized-bed reactor

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Application Number Priority Date Filing Date Title
US767557A US3037848A (en) 1958-10-16 1958-10-16 Fluidized-bed reactor

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3296205A (en) * 1962-07-16 1967-01-03 Bayer Ag Polymerization of gaseous formaldehyde
US3300299A (en) * 1963-10-07 1967-01-24 Anglo Amer Corp South Africa Segregation process

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2212120A (en) * 1939-11-24 1940-08-20 Robert D Kneale Method of roasting coffee
GB574064A (en) * 1943-12-28 1945-12-19 Shell Dev Method and converter for contacting finely divided catalysts with vapors
US2535140A (en) * 1946-09-13 1950-12-26 Universal Oil Prod Co Centrifugal separator
US2586818A (en) * 1947-08-21 1952-02-26 Harms Viggo Progressive classifying or treating solids in a fluidized bed thereof
US2684890A (en) * 1951-05-21 1954-07-27 Dorr Co Handling pulverulent materials
US2715018A (en) * 1951-12-20 1955-08-09 Dorr Co Recovery of heat from finely-divided solids
US2723838A (en) * 1952-11-15 1955-11-15 Kloeckner Humboldt Deutz Ag Apparatus for mixing and homogenizing pulverulent or fine-grained materials
US2743998A (en) * 1954-02-23 1956-05-01 Shell Dev Apparatus for the catalytic cracking of hydrocarbon oils

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2212120A (en) * 1939-11-24 1940-08-20 Robert D Kneale Method of roasting coffee
GB574064A (en) * 1943-12-28 1945-12-19 Shell Dev Method and converter for contacting finely divided catalysts with vapors
US2535140A (en) * 1946-09-13 1950-12-26 Universal Oil Prod Co Centrifugal separator
US2586818A (en) * 1947-08-21 1952-02-26 Harms Viggo Progressive classifying or treating solids in a fluidized bed thereof
US2684890A (en) * 1951-05-21 1954-07-27 Dorr Co Handling pulverulent materials
US2715018A (en) * 1951-12-20 1955-08-09 Dorr Co Recovery of heat from finely-divided solids
US2723838A (en) * 1952-11-15 1955-11-15 Kloeckner Humboldt Deutz Ag Apparatus for mixing and homogenizing pulverulent or fine-grained materials
US2743998A (en) * 1954-02-23 1956-05-01 Shell Dev Apparatus for the catalytic cracking of hydrocarbon oils

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3296205A (en) * 1962-07-16 1967-01-03 Bayer Ag Polymerization of gaseous formaldehyde
US3300299A (en) * 1963-10-07 1967-01-24 Anglo Amer Corp South Africa Segregation process

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